AU2016102428A4 - Ultra high pressure cooling and purification process and apparatus for oil production biomass syngas - Google Patents
Ultra high pressure cooling and purification process and apparatus for oil production biomass syngas Download PDFInfo
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- AU2016102428A4 AU2016102428A4 AU2016102428A AU2016102428A AU2016102428A4 AU 2016102428 A4 AU2016102428 A4 AU 2016102428A4 AU 2016102428 A AU2016102428 A AU 2016102428A AU 2016102428 A AU2016102428 A AU 2016102428A AU 2016102428 A4 AU2016102428 A4 AU 2016102428A4
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- biomass syngas
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- tar
- syngas
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- 239000002028 Biomass Substances 0.000 title claims abstract description 90
- 238000001816 cooling Methods 0.000 title claims abstract description 52
- 238000000746 purification Methods 0.000 title abstract description 22
- 238000004519 manufacturing process Methods 0.000 title abstract description 13
- 239000000428 dust Substances 0.000 claims abstract description 65
- 238000000034 method Methods 0.000 claims abstract description 45
- 239000012719 wet electrostatic precipitator Substances 0.000 claims abstract description 19
- 238000005406 washing Methods 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 56
- 238000011282 treatment Methods 0.000 claims description 18
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 6
- 239000000446 fuel Substances 0.000 claims description 5
- 238000011084 recovery Methods 0.000 abstract description 9
- 239000002918 waste heat Substances 0.000 abstract description 8
- 239000006227 byproduct Substances 0.000 abstract description 2
- 239000000571 coke Substances 0.000 abstract 1
- 238000010926 purge Methods 0.000 abstract 1
- 239000003034 coal gas Substances 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000003763 carbonization Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 230000001965 increasing effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000001376 precipitating effect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 238000010408 sweeping Methods 0.000 description 1
- 230000008685 targeting Effects 0.000 description 1
- -1 zeolite Chemical compound 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J47/00—Ion-exchange processes in general; Apparatus therefor
- B01J47/14—Controlling or regulating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/01—Pretreatment of the gases prior to electrostatic precipitation
- B03C3/014—Addition of water; Heat exchange, e.g. by condensation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/20—Apparatus; Plants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
- C10K1/046—Reducing the tar content
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1693—Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Industrial Gases (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
Abstract
PCT/CN2016/079388 An ultra high pressure cooling and purification process and apparatus for an oil production biomass syngas, the process comprising: (1) performing two-stage waste heat recovery and cyclone dust removal processing, with by-products of high pressure and low pressure steam, (2) removing a portion of heavy tar precipitated out from the biomass syngas by cooling in a second stage indirect heat exchange process, (3) further removing dust and lowering a temperature using a washing solution, (4) conducting deep removal of dust and coke using a moist air flow, and purging to remove remaining small amounts of dust and tar fog in the biomass syngas, and causing the pressure thereof to drop to 0.3-1 Mpa, so as to obtain a biomass syngas having respective dust and tar fog contents of less then 10 mg/Nm3, and a temperature of < 45°C. The apparatus is mainly comprised of an integrated heat exchange and dust removal device, a packed tower scrubber and a wet electrostatic precipitator. By optimizing process plan design and controlling appropriate process parameters, the invention realizes stepped cooling of a biomass syngas, stepped recovery of waste heat, and stepped dust removal, and achieves the object of tar removal and cooling and purification.
Description
ULTRA HIGH PRESSURE COOLING AND PURIFICATION PROCESS AND APPARATUS FOR OIL PRODUCTION BIOMASS SYNGAS
FIELD OF THE INVENTION [0001] The present disclosure relates to syngas purification technologies, and more particularly to a method and apparatus for purifying and cooling biomass syngas
BACKGROUND OF THE INVENTION [0002] With the gradual depletion of fossil fuels, the development and utilization of renewable and clean biomass energy have received more and more attention and are under rapid development, and thus syngas and oil production with biomass has become an important research topic in the field of new energy development [0003] Similar to the gas production with coal, the syngas production with biomass also necessitates the cooling, dedusting and other purification processes. At present, there are many researches on the methods of biomass gasification to produce syngas, but there are few researches on how to cool and purify biomass syngas. In most cases, the traditional method for cooling and washing coal gas is followed. The traditional method for preliminarily cooling coal gas includes indirect preliminary cooling, direct preliminary cooling, and indirect/direct preliminary cooling. The preliminary cooling mainly comprises cooling the coal gas exiting from a carbonization chamber to 22-35°C before it enters an electric tar trapper. During an indirect preliminary cooling process, the coal gas does not contact the cooling medium directly, only indirect heat transfer occurs between the two phases, and no mass transfer takes place; and the cooling and purification effects on the coal gas are good. During a direct preliminary cooling process, the coal gas is in direct contact with the aqueous ammonia sprayed, and both mass and heat transfer take place. Compared with the indirect preliminary cooling, the direct preliminary cooling has the characteristics of high cooling efficiency for coal gas, small resistance, low equipment cost, and large power consumption. The indirect/direct preliminary cooling is a combined process in which the coal gas is cooled indirectly and then directly, and which
2016102428 15 Apr 2016
PCT/CN2016/079388 incorporates the advantages of both indirect and direct cooling. In addition, many coal gas dedusting methods are available, including precipitation, filtration, cyclone dust collection, electrostatic dust collection, water scrubbing or Venturi dust removal. The dust removal efficiency and resistance vary greatly with different processes.
[0004] In the conventional gas production with coal, the temperature of the crude coal gas exiting from the carbonization chamber is about 650°C; and the temperature of the syngas at an outlet of a modem fluidized bed biomass gasifier is generally 950°C or above, which is far greater than the temperature of the coal gas at the outlet of the carbonization chamber. If the method for preliminarily cooling coal gas is copied ignoring the fact that the temperature of the syngas at the outlet during the syngas production with biomass is higher than the temperature of the coal gas at the outlet during the gas production with coal, it is obvious that the cooling effect and the purification index of the biomass syngas cannot be achieved. Moreover, if the traditional method for purifying coal gas is simply simulated, there are still defects such as complex system, long process, high energy consumption, low efficiency, and poor stability and economy. Therefore, it is necessary to provide a cooling and purification process and apparatus for syngas produced in a biomass gasifier.
SUMMARY OF THE INVENTION [0005] In view of the above-described problems, it is one objective of the invention to provide a method and apparatus for purifying and cooling biomass syngas for oil production. Using the process and apparatus, the syngas experiences multi-stage treatments at a defined particular temperature under a defined particular pressure. The method is stable and efficient in cooling and purification, and the apparatus has relatively low manufacturing cost.
[0006] To achieve the above objective, in accordance with one embodiment of the invention, there is provided a method for purifying and cooling biomass syngas, the method comprising:
2016102428 15 Apr 2016
PCI7CN2016/079388 [0007] 1) cooling biomass syngas having a temperature of 950°C or higher and a pressure of 3.0 mPa or higher output from a fluidized bed gasifier to 520-5 80°C using a first-stage indirect heat exchange with process water, and recycling waste heat to yield a first steam; then subjecting the biomass syngas to cyclone dust removal treatment; and further cooling the biomass syngas to a temperature of < 210°C using a second-stage indirect heat exchange with process water, and recycling waste heat to yield a second steam;
[0008] 2) collecting and removing a portion of heavy tar precipitating out of the biomass syngas during the second-stage indirect heat exchange;
[0009] 3) carrying out dust removal and cooling using a scrub solution, to scrub off most of dust, tar droplets, and water soluble gases from the biomass syngas after the heat exchange and dust removing treatment, in which the temperature of scrubbed biomass syngas is controlled at 43-47°C; and [0010] 4) conducting deep removal of dust and tar with a wet gas stream, to sweep off remains of dust and tar fog in the scrubbed biomass syngas, and allowing the pressure to drop to 0.3-1 mPa, to obtain a cleaned biomass syngas having a dust and tar content of less than 10 mg/Nm3, and a temperature of below 45°C; a sensible heat recovery rate of the biomass syngas being greater than 80%.
[0011] In a class of this embodiment, in 1), during the first-stage indirect heat exchange, the biomass syngas is cooled to 550-570°C; and during the second-stage indirect heat exchange, the biomass syngas is cooled to 65-95°C.
[0012] In a class of this embodiment, in 1), during the first-stage indirect heat exchange, the biomass syngas is cooled to 555-565°C; and during the second-stage indirect heat exchange, the biomass syngas is cooled to 65-75°C.
[0013] In a class of this embodiment, in 1), the pressure of the first steam generated is 6.0-9.8 mPa, and the pressure of the second steam generated is 0.5-0.8 mPa.
[0014] In a class of this embodiment, in 1), the pressure of the first steam generated is 6.0-8.5 mPa, and the pressure of the second steam generated is 0.5-0.8 mPa.
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PCI7CN2016/079388 [0015] In a class of this embodiment, in 1), the first steam generated is fed back to the fluidized bed gasifier, and used as a gasifying agent of a biomass fuel.
[0016] In a class of this embodiment, in 1), the biomass syngas output from the fluidized bed gasifier is controlled to have a temperature of 1000-1200°C, a pressure of 3.0-4.0 mPa, a dust content of < 20 g/Nm3, and a tar content of < 3 g/Nm3.
[0017] In a class of this embodiment, in 1), the second steam generated is used in 4) as a wet gas stream to sweep off the dust and tar fog in the biomass syngas.
[0018] In accordance with another embodiment of the present disclosure, there is provided an apparatus for purifying and cooling biomass syngas for oil production, the apparatus comprising an integrated heat exchange and dust removal device, a packed tower scrubber, and a wet electrostatic precipitator. The integrated heat exchange and dust removal device has an overall structure comprising sequentially a first heat exchanger, a cyclone separator, and a second heat exchanger connected in compact tandem. A gas inlet of the first heat exchanger is connected to a syngas outlet of a fluidized bed gasifier, a gas outlet of the second heat exchanger is connected to a gas inlet of the packed tower scrubber, a gas outlet of the packed tower scrubber is connected to an input port of the wet electrostatic precipitator, and an output port of the wet electrostatic precipitator is connected to a gas inlet of a gas tank.
[0019] In a class of this embodiment, a steam outlet of the first heat exchanger is connected to a gasifying agent inlet of the fluidized bed gasifier via a first steam conveying pipe.
[0020] In a class of this embodiment, a steam outlet of the second heat exchanger is connected to a wet gas stream inlet of the wet electrostatic precipitator via a second steam conveying pipe.
[0021 ] In a class of this embodiment, a dust outlet at a bottom of the cyclone separator is connected to a feed inlet of a bin pump, and a feed outlet of the bin pump is connected to an ash storage tank.
[0022] In a class of this embodiment, a tar outlet at a bottom of the second heat exchanger is connected to a feed inlet of a tar trough.
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PCT/CN2016/079388 [0023] In a class of this embodiment, the output port of the wet electrostatic precipitator is further connected to a gas inlet of a tail gas incinerator.
[0024] Compared with the prior art, the method and apparatus for purifying and cooling biomass syngas of the present disclosure has the following advantages.
[0025] 1. In the present disclosure, the temperature of the biomass syngas is defined at 950°C or higher, and the biomass syngas is subjected to multi-stage treatments under a pressure of 3.0 mPa or higher; and the high-pressure steam having a pressure of 6.0-9.8 mPa generated during the waste heat recovery is used as a gasifying agent of a biomass fuel. These allow the whole cooling and purification system to operate under an extra-high pressure, such that the gas flow rate is increased while the cooling and purification effects are ensured, thereby shortening the process flow and the treatment time, and greatly increasing the treatment efficiency. As a result, the whole treatment system is simple, and has a smooth process, a high cooling efficiency, a good purification effect, low energy consumption and good economic benefits. Especially, the use of high-pressure steam with a pressure of 6.0-8.5 mPa as a gasifying agent of a biomass fuel has resulted in an unexpected cooling and purification effect.
[0026] 2. The cooling and purification process of the present disclosure includes two stages of cooling. In the first stage, the biomass syngas is cooled to 520-580°C, a temperature that is controlled to be above the condensation point of heavy tar, to avoid the condensation of tar in this stage. In the second stage, the biomass syngas is cooled to < 210°C, so as to condensate and collect the heavy tar in this stage. Moreover, the biomass syngas is subjected to cyclone dust removal treatment in between the two stages. In this way, the massive collection and treatment of heavy tar are achieved, and quite good treatment conditions are also provided for subsequent dedusting treatment. After two stages of waste heat recovery under two different pressures, further dust removal and cooling, and deep removal of the tar are carried out, to finally obtain a treated biomass syngas with a dust level of < 10 mg/Nm3, a tar content of < 10 mg/Nm3, and a temperature of < 45°C, in which the sensible heat recovery rate is greater than 80%, and high- and low-pressure steam are obtained as by-products.
2016102428 15 Apr 2016
PCI7CN2016/079388 [0027] 3. In the present disclosure, the biomass syngas is subjected to a slag solidification treatment in the gasifier, in which the high-pressure steam is used as a gasifying agent for providing pressure. That is, the high-pressure steam generated in the integrated heat exchange and dust removal device is input into the biomass gasifier as a gasifying agent for providing pressure to the purification apparatus. By adjusting the pressure of the steam, it can be ensured that the pressure head at an outlet of the biomass gasifier overcomes the resistance in the cooling and purification apparatus and maintains a positive pressure of 0.3-1 mPa (G) when reaches the gas inlet of the gas tank. In this way, the gasifier, the integrated heat exchange and dust removal device, the packed tower scrubber, the wet dust collector and other units are ensured to operate under a positive pressure, thereby preventing external air from leakage into the cooling and purification apparatus, and reducing the possibility of gas explosion; and further, the blower in the gasification procedure and the air compressor in the synthesis procedure are omitted, thus greatly reducing the overall energy consumption in the gasification and oil synthesis procedures, and solving the problems such as complex system, long process, high energy consumption, low efficiency, poor stability and economy, and low targeting performance existing in the traditional gas purification process.
[0028] 4. In the apparatus of the present disclosure, an integrated heat exchange and dust removal device is adopted, in which high-temperature heat exchange and low-temperature heat exchange are arranged integrally, and a cyclone separator is built in therebetween, so the structure is compact to save the material, and the heat exchange efficiency is high, thereby greatly enhancing the treatment efficiency of the cooling and purification process. The dust and tar levels in the biomass syngas are relatively low, and preliminary dust removal is provided between two stages of heat exchangers by using the cyclone separator coming with the integrated heat exchange and dust removal device, thus greatly improving the dust removal efficiency. After the first-stage indirect heat exchange, the dust removal efficiency of the cyclone separator can be up to 90% or higher when the biomass syngas is cooled to 550-570°C; and the dust removal efficiency of the cyclone separator can be up to 99.9% or higher when the biomass syngas is cooled to 555-565°C.
2016102428 15 Apr 2016
PCI7CN2016/079388 [0029] 5. Preliminary dust removal can be achieved by the integrated heat exchange and dust removal device, so as to save quantities of flushing water and energy consumption for water treatment, and also save the water treatment equipment. Moreover, the device is simple in arrangement and easy to operate, and materials are salved, resulting in considerable economic benefits.
BRIEF DESCRIPTION OF THE DRAWINGS [0030] FIG. 1 is a schematic diagram of an ultrahigh-pressure cooling and purification apparatus for biomass syngas in accordance with one embodiment of the present disclosure.
DETAILED DESCRIPTION OF THE EMBODIMENTS [0031] For further illustrating the invention, experiments detailing a method and apparatus for purifying and cooling biomass syngas are described below. It should be noted that the following examples are intended to describe and not to limit the invention.
[0032] FIG. 1 shows an ultrahigh-pressure cooling and purification apparatus for biomass syngas for oil production. The apparatus comprises an integrated heat exchange and dust removal device 2, a packed tower scrubber 3 and a wet electrostatic precipitator
4. The integrated heat exchange and dust removal device 2 has an overall structure comprising sequentially a high-temperature heat exchanger 2a, a cyclone separator 2b, and a low-temperature heat exchanger 2c connected in compact tandem. A gas inlet 2-1 of the high-temperature heat exchanger 2a is connected to a syngas outlet 1-1 of a fluidized bed gasifier 1, a gas outlet 2-2 of the low-temperature heat exchanger 2c is connected to a gas inlet 3-1 of the packed tower scrubber 3, a gas outlet 3-2 of the packed tower scrubber 3 is connected to an input port 4-1 of the wet electrostatic precipitator 4, and an output port 4-2 of the wet electrostatic precipitator 4 is connected to a gas inlet 5-1 of a high-pressure gas tank 5, which is a spherical ultrahigh-pressure gas tank. A high-pressure steam outlet of the high-temperature heat exchanger 2a is connected to a gasifying agent inlet 1-2 of the fluidized bed gasifier 1 via a high-pressure steam
2016102428 15 Apr 2016
PCT/CN2016/079388 conveying pipe 6. A low-pressure steam outlet of the low-temperature heat exchanger 2c is connected to a wet gas stream inlet 4-3 of the wet electrostatic precipitator 4 via a low-pressure steam conveying pipe 7. A dust outlet 2-3 at a bottom of the cyclone separator 2b is connected to a feed inlet 9-1 of a bin pump 9, and a feed outlet 9-2 of the bin pump 9 is connected to an ash storage tank 10. A tar outlet 2-4 at a bottom of the low-temperature heat exchanger 2c is connected to a feed inlet 11-1 of a tar trough 11. The output port 4-2 of the wet electrostatic precipitator 4 is further connected to a gas inlet 8-1 of a tail gas incinerator 8.
[0033] A process implemented with the above equipment is as follows. A high-temperature ultrahigh-pressure biomass syngas output from the fluidized bed gasifier 1 is controlled to have a temperature of 1000-1200°C, a pressure of 3.0-4.0 mPa, a dust level of <20 g/Nm3, and a tar content of < 3 g/Nm3. The high-temperature ultrahigh-pressure biomass syngas is led out via the syngas outlet 1-1 at a top of the gasifier 1 after the slag solidification treatment in the gasifier, and then enters the integrated heat exchange and dust removal device 2. The biomass syngas is subjected to a first-stage indirect heat exchange in the high-temperature heat exchanger 2a to cool the high-temperature ultrahigh-pressure biomass syngas output from the gasifier 1 to 520-580°C, preferably to 550-570°C, and further preferably to 555-565°C. The high-pressure steam of 6.0-9.8 mPa and preferably 6.0-8.5 mPa generated during the waste heat recovery is delivered to the gasifier 1 and used as a gasifying agent of a biomass fuel. Subsequently, the high-temperature ultrahigh-pressure biomass syngas experiences a cyclone dust removal treatment by the cyclone separator 2b in the integrated heat exchange and dust removal device 2, and then enters the low-temperature heat exchanger 2c for a second-stage indirect heat exchange, such that the biomass syngas is further cooled to a temperature of < 210°C, preferably to 65-95°C, and more preferably to 65-75°C in the integrated heat exchange and dust removal device 2. The low-pressure steam of 0.5-0.8 mPa generated during the waste heat recovery is supplied to the exterior. A portion of heavy tar precipitating out of the biomass syngas upon cooling during the second-stage indirect heat exchange process flows via the tar outlet 2-4 at the bottom of the low-temperature heat exchanger 2c into the tar trough 11, and removed by collection in the tar trough 11. Next, the cooled and preliminarily-dedusted
2016102428 15 Apr 2016
PCT/CN2016/079388 biomass syngas exits from the integrated heat exchange and dust removal device 2 via the gas outlet 2-2, and enters the packed tower scrubber 3 via the gas inlet 3-1 of the packed tower scrubber 3, where the biomass syngas is further dedusted and cooled by using an alkaline scrub solution such as caustic soda and a filler such as zeolite, to scrub most of the dust, tar droplets, and water soluble gases off from the biomass syngas, in which the temperature of the scrubbed biomass syngas is cooled to 43-47°C. Finally, the scrubbed biomass syngas is led out of the packed tower scrubber 3 via the gas outlet 3-2, and input into the wet electrostatic precipitator 4 via the input port 4-1 of the wet electrostatic precipitator 4; and the low-pressure steam generated during the second-stage indirect heat exchange process is also introduced therein as a wet gas stream for sweeping the dust and tar fog in the biomass syngas. The deep removal of dust and tar allows a small amount of dust and tar fog remaining in the biomass syngas to be removed, and allows the pressure of the biomass syngas to drop to 0.3-1 mPa, so as to obtain a cleaned biomass syngas having a dust and tar content of less than 10 mg/Nm3, and a temperature of below 45°C, with a sensible heat recovery rate being greater than 80%. Moreover, the qualified biomass syngas is delivered to the ultrahigh-pressure gas tank 5 via the gas inlet 5-1 of the ultrahigh-pressure gas tank 5 for storage or for use in a downstream procedure. The exhaust gas is disposed in the tail gas incinerator 8 connected in parallel with the ultrahigh-pressure gas tank 5, during which a low-pressure steam is generated and supplied to the exterior. The dust separated by the cyclone separator 2b in the integrated heat exchange and dust removal device 2 is collected by the bin pump 9 and then pneumatically conveyed to the ash storage tank 10 for storage and later reasonable utilization. The positive pressure of 0.3 mPa or higher remains at the gas inlet 5-1 of the high-pressure gas tank 5, to ensure that the integrated heat exchange and dust removal device 2, the packed tower scrubber 3, the wet electrostatic precipitator 4 and the ultrahigh-pressure gas tank 5 can operate under an ultrahigh pressure.
Claims (14)
1) cooling biomass syngas having a temperature of 950°C or higher and a pressure of 3.0 mPa or higher from a fluidized bed gasifier to a temperature of 520-580°C using a first-stage indirect heat exchange, to yield a first steam;
subjecting the biomass syngas to cyclone dust removal treatment;
cooling the biomass syngas to a temperature of < 210°C using a second-stage indirect heat exchange, to yield a second steam and heavy tar;
1. A method for purifying and cooling biomass syngas, the method comprising:
2. The method of claim 1, characterized in that in 1), during the first-stage indirect heat exchange, the biomass syngas is cooled to 550-570°C; and during the second-stage indirect heat exchange, the biomass syngas is cooled to 65-95°C.
2) collecting the heavy tar evolved out of the biomass syngas during the second-stage indirect heat exchange process, and removing a portion of the heavy tar;
3. The method of claim 1, characterized in that in 1), during the first-stage indirect heat exchange, the biomass syngas is cooled to 555-565°C; and during the second-stage indirect heat exchange, the biomass syngas is cooled to 65-75°C.
PCT/CN2016/079388
2016102428 15 Apr 2016
3) washing and cooling the biomass syngas using a scrub solution, to scrub off dust, tar droplets, and water-soluble gases from the biomass syngas, wherein a temperature of scrubbed biomass syngas is between 43 and 47°C; and
4. The method of claim 1, 2 or 3, characterized in that in 1), the pressure of the first steam is 6.0-9.8 mPa, and the pressure of the second steam is 0.5-0.8 mPa.
4) conducting deep removal of dust and tar with a wet gas stream, to remove dust and tar in the scrubbed biomass syngas, and allowing the pressure to drop to 0.3-1 mPa, to obtain a cleaned biomass syngas having a dust and tar β
content of less than 10 mg/Nm , and a temperature of below 45°C.
5. The method of claim 1, 2 or 3, characterized in that in 1), the pressure of the first steam is 6.0-8.5 mPa, and the pressure of the second steam is 0.5-0.8 mPa.
6. The method of claim 1, 2 or 3, characterized in that in 1), the first steam generated is fed back to the fluidized bed gasifier, and used as a gasifying agent of a biomass fuel.
7. The method of claim 1, 2 or 3, characterized in that in 1), the biomass syngas output from the fluidized bed gasifier is controlled to have a temperature of 1000-1200°C, a pressure of 3.0-4.0 mPa, a dust content of < 20 g/Nm3, and a tar content of < 3 g/Nm3.
8. The method of claim 1, 2 or 3, characterized in that the second steam produced in 1) is used in 4) as a wet gas stream to sweep off the dust and tar in the biomass syngas.
9. An apparatus for purifying and cooling biomass syngas, the apparatus comprising:
an integrated heat exchange and dust removal device (2);
a packed tower scrubber (3); and a wet electrostatic precipitator (4);
characterized in that the integrated heat exchange and dust removal device (2) comprises a first heat exchanger (2a), a cyclone separator (2b), and a second heat exchanger (2c) connected in compact tandem in sequence; and
2016102428 15 Apr 2016
PCI7CN2016/079388 a gas inlet (2-1) of the first heat exchanger (2a) is connected to a syngas outlet (1-1) of a fluidized bed gasifier (1), a gas outlet (2-2) of the second heat exchanger (2c) is connected to a gas inlet (3-1) of the packed tower scrubber (3), a gas outlet (3-2) of the packed tower scrubber (3) is connected to an input port (4-1) of the wet electrostatic precipitator (4), and an output port (4-2) of the wet electrostatic precipitator (4) is connected to a gas inlet (5-1) of a gas tank (5).
10. The apparatus of claim 9, characterized in that a steam outlet of the first heat exchanger (2a) is connected to a gasifying agent inlet (1-2) of the fluidized bed gasifier (1) via a first steam conveying pipe (6).
11. The apparatus of claim 9 or 10, characterized in that a steam outlet of the second heat exchanger (2c) is connected to a wet gas stream inlet (4-3) of the wet electrostatic precipitator (4) via a second steam conveying pipe (7).
12. The apparatus of claim 9 or 10, characterized in that a dust outlet (2-3) at a bottom of the cyclone separator (2b) is connected to a feed inlet (9-1) of a bin pump (9), and a feed outlet (9-2) of the bin pump (9) is connected to an ash storage tank (10).
13. The apparatus of claim 9 or 10, characterized in that a tar outlet (2-4) at a bottom of the second heat exchanger (2c) is connected to a feed inlet (11-1) of a tar trough (11).
14. The apparatus of claim 9 or 10, characterized in that the output port (4-2) of the wet electrostatic precipitator (4) is further connected to a gas inlet (8-1) of a tail gas incinerator (8).
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| CN201510355110.4 | 2015-06-24 | ||
| CN201510355110.4A CN104927925B (en) | 2015-06-24 | 2015-06-24 | Biomass synthesis gas super-pressure cooling and purifying technique and its equipment for liquefaction |
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| AU2016102428A Ceased AU2016102428A4 (en) | 2015-06-24 | 2016-04-15 | Ultra high pressure cooling and purification process and apparatus for oil production biomass syngas |
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| AU2016283230A Pending AU2016283230A1 (en) | 2015-06-24 | 2016-04-15 | Ultra high pressure cooling and purification process and apparatus for oil production biomass syngas |
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| EP (1) | EP3315588A4 (en) |
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| CN104927925B (en) * | 2015-06-24 | 2017-11-14 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesis gas super-pressure cooling and purifying technique and its equipment for liquefaction |
| CN108554111A (en) * | 2017-07-08 | 2018-09-21 | 重庆金环生物质能有限公司 | The instantaneous cooling purifier system and technique for being automatically separated biogas, tar of classification water cycle |
| CN107603677B (en) * | 2017-11-07 | 2020-11-20 | 山东京博众诚清洁能源有限公司 | Coal gas production equipment and safe blow-in method thereof |
| CN108413405B (en) * | 2018-03-20 | 2019-11-22 | 江苏蓝电环保股份有限公司 | The garbage combustion device of exhaust gas wet dust removal |
| CN110055113B (en) * | 2018-05-18 | 2023-12-12 | 新能能源有限公司 | Pretreatment system for crude gas produced by fluidized bed gasifier |
| CN109708989B (en) * | 2018-12-28 | 2021-10-01 | 扬州大学 | Device for measuring contents of oil, water and particulate matters in gas and using method thereof |
| CN110608927B (en) * | 2019-09-27 | 2024-07-05 | 广东省特种设备检测研究院珠海检测院 | Tar sampler in biomass gasification fuel gas and working method thereof |
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| DE3217366A1 (en) * | 1982-05-08 | 1983-11-10 | Metallgesellschaft Ag, 6000 Frankfurt | METHOD FOR PRODUCING A MOST INERT-FREE GAS FOR SYNTHESIS |
| JP2000328070A (en) * | 1999-03-12 | 2000-11-28 | Ube Ind Ltd | Waste gasification treatment method |
| JP2004182903A (en) * | 2002-12-04 | 2004-07-02 | Kawasaki Heavy Ind Ltd | Method and apparatus for gasifying biomass |
| JP5217295B2 (en) * | 2007-08-08 | 2013-06-19 | 株式会社Ｉｈｉ | Coal gasification gas purification method and apparatus |
| CN101280223A (en) * | 2008-04-14 | 2008-10-08 | 山东联合能源技术有限公司 | Integrated gasification combined cycle thermoelectric oil gas multi-production process for efficient clean region |
| CN101285006B (en) * | 2008-05-30 | 2011-10-05 | 中国五环工程有限公司 | Gasification process of water/gas mixed partial-chilled dry powder fuel and device |
| JP2011105890A (en) * | 2009-11-20 | 2011-06-02 | National Institute Of Advanced Industrial Science & Technology | Circulating fluidized bed gasification reactor |
| CN101781586B (en) * | 2010-01-29 | 2013-06-26 | 上海锅炉厂有限公司 | High-temperature synthesis gas sensible heat recovery device |
| CN102604685B (en) * | 2011-12-29 | 2014-11-26 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesis gas positive pressure purification process and system configuration for oil production |
| CN102618330B (en) * | 2011-12-29 | 2014-02-26 | 武汉凯迪工程技术研究总院有限公司 | High temperature normal pressure biomass gasification island process |
| CN102585916B (en) * | 2011-12-29 | 2014-11-26 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesized gas negative pressure purifying process method and system configuration for producing oil |
| CN103265979B (en) * | 2013-06-03 | 2015-04-08 | 武汉凯迪工程技术研究总院有限公司 | Technology and device for cooling and purifying high-temperature and high-pressure biomass synthesis gas |
| CN103409175A (en) * | 2013-08-12 | 2013-11-27 | 浙江大学 | Purifying and tar recovery system for high temperature gas containing ash and tar and method thereof |
| CN104927925B (en) * | 2015-06-24 | 2017-11-14 | 武汉凯迪工程技术研究总院有限公司 | Biomass synthesis gas super-pressure cooling and purifying technique and its equipment for liquefaction |
| CN204737925U (en) * | 2015-06-24 | 2015-11-04 | 武汉凯迪工程技术研究总院有限公司 | A living beings synthetic gas superhigh pressure cooling clarification plant for making oil |
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2015
- 2015-06-24 CN CN201510355110.4A patent/CN104927925B/en active Active
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2016
- 2016-04-15 AU AU2016283230A patent/AU2016283230A1/en active Pending
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- 2016-04-15 JP JP2017566412A patent/JP6612366B2/en not_active Expired - Fee Related
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| CN104927925A (en) | 2015-09-23 |
| EP3315588A1 (en) | 2018-05-02 |
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| JP2018526478A (en) | 2018-09-13 |
| AU2016283230A1 (en) | 2018-01-18 |
| CA2989906A1 (en) | 2016-12-29 |
| US20180105759A1 (en) | 2018-04-19 |
| RU2018102556A3 (en) | 2019-07-24 |
| CN104927925B (en) | 2017-11-14 |
| JP6612366B2 (en) | 2019-11-27 |
| WO2016206453A1 (en) | 2016-12-29 |
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